Apparatus for controlling the concentration of noncondensable gases in an absorption refrigeration system



2,610,482 CENTRATION 2 SHEETSSHEET 1 INVENTOR E- BERRY N APPARATUS FOR CONTROLLING THE CON OF NONCONDENSABLE GASES IN AN ABSORPTION REFRIGERATION SYSTEM Sept. 16, 1952 Flled Aprll 28 1949 Sept. 16, 1952 N. E. BERRY 2,610,482

. I APPARATUS FOR CONTROLLING THE CONCENTRATION OF NONCO NDENSABLE GASES IN AN ABSORPTION REFRIGERATION SYSTEM I 2 SHEETS-SHEET 2 Filed April 28, 1949 I v INVENTORJ.

Patented Sept. i6, i952 Al mnh ms FOR CO TR LEHQGJ GENTRATI'QN OF NONCONDENSABLE' jGASESiIN ANY ABSORRTIONYREERIGERAF- H N S$E TEM N'oiftgn EgBlerry, 'Newbu T-he lpresent invention! relates. to refrigeration jandmurepafticul-arly to contrdllingetheconcentmtiqn o'fnoneeonden'sable ,gases at two-presfsufelebsorpti'on refrigeratiqn system.

In vacuum type absorption: refrigeration systems: such as -illi1stra. ted and deseribed in the Umteistates Letters Petehtte .AlbertR; Thomas et 1; No. 2,282,503. lssued;May-12; 11942. ana m- ,,titled Refrigeration,non cendensable gases rare tipt to accumulate ;in,..the .ccpndenseifl'az ndwv absorber end act gs an insulating barrier preventing the transfer of heat ,thrgugh those parts which they blanket ,By continually withdrawing the gases i m h i pa t h -wWmih diffimilii t p rienc i mm th c mu n aq -n ass i -a idedbu i iiqlln ha ihs w h l e oun iQii esi t nessy iesi es zhel we v ed t imi s 't-mimm m the t, 1 1 91 s rheet 1t na ihv v s e o ms ing @015 a in $5 1 e l iq ef 1 1 99- I as f6 V; )g:-.Y $1 n p d fiQQI-m 5%35 durin Per l-e s i Q Q iQH an e v n 4 fl 9 429 rtll 'sfi e e w e 'pe dsop a io uq enke rangement re duces sup erheeting-j with 515 attendant nqisei and -i -rre gu;ler ,eimulatiqn :o f sgluti qn wring-s i s l t o pnera i nnb dufin Pml ns di e rd dnereiid eidua ?ea ily-th s s m i e ed abe .ih -h iniinsm emq m nequired to; rpreventivsu-pei'heatting.

Qne-ofth fobjects f the resent inventignis Jiloipiwide n Jen-F min L li n ibs hi" v itiebmtionsystew t p- 'ppeven'ting the eec'qrnul ai j ex e s e meunts se w l st l leime in u ng h pr sen Qi imaml emquntiq gas in the system.

type indieatcl which continuously .withd aws gas item the ;system.and returns gas to the low pressure. side at; a. phedtefminedslow rate ior direct Contact withnsolution in the. absorber.

Anbther object is to, provide apparatus .of the "typeindicaited which continuously withdraws gets iirqmthe system duIiIlgWOIfkiflg eyglesand is openable vafter a predetermined amount of gas has ,b een wi'thdr awn i to deliver measured quantities l ro c pies ut sp t e j ch as'l hi o'f 'gals ,b'eckto the lew pressure side of thesyste n.

. s l anqt mect f he-i ve tioni r pr ,vide anapparatus-of the type indicated ier withdrawingjrgas. from an active part of the system a.t-a rate ,ptpportionel to the eqneentration, 40f

snhsriq' e su A weep fi- Lg as thereimdeliverihggas to the systemat a. prefle vm i esis w rats n transferring assesse --tq;a storagevessel after apredeterminedemount has: accumulated in s the apparatus.

.Th se ahd'0the1' Objeets will become apparent i h stem;

llivefinQabSpnptiunsol ti on te ant lled i' te.

7 Another object is, to provide apparatus 9f; the 335 7' Q'Qber lhtherebetween. "Aheating medium sue '2 y. from the followingqdesc z iption jan 'l.v

drawn. tip which like reference.charactersvden te lik pests throughout the several views. It is tpfbe'fextiprlessly understood, 'hqwever, that the (1 a e io the purp se o illu t at on ;on1Ye a, clefinition of the limitsfofjthe-rintientio erence being hadfor thislpurposetpthe ppe (1 claims. In 'thefirawihgst V t F em mmefii w 1. a iab ornilgn refrigeratiQ-nEsyStem incprpgretin'g the apparatus of the present invfinl ion for eqhtrqlling the. g centration, of non con densable gases. in {the ltem;

Fig. '2 is an enlarged sectional view pithe gas receiving vessel illusti atedlinrffi a the sibhomtllhe a d astnep thex i T1 1" envening measured guantitiesofg ags frqmthe y to thesystem; fig. 3 is, a view similar to figtll'showing en apparatus of modifiedv censtructi'oh fpr cen re!- ling the concentratien of non-eonqensahlei es Linthe system;

Fig.. 4 shows the modified .tcqnstruetion seconda y r pumpo d li eries eels Fig. '5 is e sectional View of}, secondery pu fge .pump pf modified consfi uqti niand Big; sis .an..e'nla 17 .o when written In the drawings PI BYwn ratu iQMh invention, is shqwn :app ied...to .s fqw" .Qvacuum'; type absorption rejrigei atien; system, pf h kind lfa de nd, 1 r be ,i nthe!fh h et-ial, patent referred to gipove. IPrefei abl Sys m 1 71 1265 water as ia refwrisera t' g h m sleas an; s rb nt fr ge t .sx tem. sbii prises e, generatonia cpndensei ifi an eyapeg'atpr 1, an. absorber} and a, heat eggehafigef Q-intetconnected m ro idenalh 9 flew fi eIi and absorbent ,Thegeneretqn Sfhes a? 'Iureilt'y lj u ri h u e im QOI MQW -a the g sw i t an in et: emb en less: 9m E f0 aseperet' gchamhentl. The tubes Lilla "clos d i a acke l3 i 1 rqv dea. new ri zit st emiis, sup lies mineswhen ro eblen-source; thr ughe eq e iitj figaeqa' m??? '1 ma n n thefitsem n the, champ is provided adjacent t-helower enclpf g hchambervlfl. l 5"} i,

, hes neshe b L otlsesee et 1 ,is nnei leee e i smhm' rid the condenser, in turn, is connected to the evaporator 1 by a conduit l9 having an orifice 20 therein. The orifice 23 in the conduit I9 is of such size as to pass .all of the liquid refrigerant condensed in the condenser 6 and permit a limited flow of refrigerant vapor therethrough to purge non-condensable gases from the condenser, as claimed in my co-pending application for Letters Patent, Serial No. 725,000, filed January 29, 1947 and entitled Refrigeration.

Evaporator 1 comprises a plurality of substantially horizontal tubes 2| extending between headers 22 and 23, A cup 24 is provided at one end of each tube 2| in the heade 22 or 23 to receive liquid refrigerant flowing from the tube above so that refrigerant flows successively through the tubes from the top to the bottom of the evaporator. The headers 22 and 23 open into the top of the absorber 8 to provide a path ,forthe flow of refrigerant vapor from the evap- :smtor1torne absorber. The absorber 8 is in lthe form of a tank having a bank of vertically arranged cooling coils 25 therein to which cooling l-wiatjer'is supplied through the header 26 and supply. pipe 21 from any suitable source such as ;a city water main, cooling tower or th like. Each cooling coil 25 is-in the form of a plurality of, substantially horizontal pipes or tubes arirang'ed'one over the other with their ends connected to provide a continuous path of flow from the bottom to the top of the coil. Cooling water fronithe bank of cooling coils 25 is delivered "through a header 28 and conduit 29 to the inlet lofcor'idenser' 6.. .'Absorption solution weak in refrigerant or, in other words, concentratedvsalt solution flows by gravity from separating chamber I2 'to the top .of .the absorber -8 in a path of flow including a lcond'uit .30, heat, exchanger 3, conduit 3| and .liquid distributor 32. The liquid distributor 32 deliversabsorption solution ontothe uppermost tube of each coil 25 in a series of spaced drops .which flow over. the surface of the tube in a thin and then drop and spread over the surface ofthe next lowermost tube successively from the "top' to'thebottom of each coils This division of the absorption solution provides a large area Qof solution for contact with refrigerant vapor and also provides for ithe'transfer of the heat of ab- Qsorpubn to" the cooling water, throughout the entire surface area of the coils.

:otherwords, dilute salt solution flows by gravity j fr oin th e bottom of 'the absorber B .to the inlet chamber 'H of the generator. in a path of flow including; a conduit'33,,heat exchanger 3, con-'- duit 34, reservoir vessel'35 and conduit 36. The reservoir vessel 35 is positioned above th base ,of: the generator 5 to continuously supply absorption solution to the inlet chamber H and maintain a liquid column in conduit 36 to proflvide. a reaction head on the solution in the gen- -erator tubes |0. To conserve space the reservoir vessel 35'is of annular form and surrounds the Jacket I3 of the generator 5. Preferably, the vessel 35 is of such dimensions as to receive vary- ,i1n"g1" amounts of solution without materially affecting the liquid level therein to maintain a sirbstantially constant reaction head, the top o-f ,the ve'ssel 35. being connected to the separating pressure corresponding substantially to the vapor 4 perature and the evaporator and absorber 8 cperate at a lower pressure corresponding to the vapor pressure of the refrigerant in the absorption solution at the temperature and concentration of the solution in the absorber. The difference in pressures in the condenser E and evaporator I is maintained by the orifice 20 and the difference in pressures in the absorber 8 and generator 5 is maintained by liquid columns in the conduits 3| and 33. The liquid level in'the conduit 33 is indicated by the reference character the evaporator by a. conduit 42.

end-of the'concentration control vessel 40 is connectedto the inlet chamber ll of the generator 5 by a conduit 43.

V In such a system it has been found that noncondensable gases are apt to occur which if allowed to accumulate in the condenser 6 and absorberl8 willreduce the-transfer of heat in'the elements. On the other hand,'it has been found "that if all of thenon-condensable gases arewithdrawn from the system, the boiling of the solution inpthe generator tubes I0 is erratic which produces undesirable noise and irregular lifting of absorption solution. It is believed that when gas is present in the absorber a small quantity is trapped in solution as the latter flows into conduit 33 which providesa nucleus to promote boiling in the generator but when no gas is available the solution superheats in the generatorcausing the noise and irregular pumping' In a'ccorda ncewith the present invention apparatus is provided for continuously withdrawing jnon-condensable' gas from the low pressure side of the system to prevent its accumulation therein and delivering atleast a part of such withdrawn I; Absorption solution strong in refrigerant or; in

gas back to the low pressureside of the system at a slow rate to insurethe presence of a minimum amount of gasin the absorber at all times. The apparatus comprises a purge device 45 for continuously withdrawing gases from the low pressure side, a vessel 46 for receiving liquid and gas fron thepurge device and means in the vessel for delivering gas-from the vessel back to the low pressure side of the system.

v 1 The purge device 45 is generallysirnilar to that illustrated and described'inUnited States Let- "ters Patent to C. S. Roswell, No, 2,384,861, issued September l8, 1945 and consists of a vessel 41 connected'tothe interior of'the main absorber e by a suction tube'48. :The bottom of the vessel 4? is formed to provide a small cup or sump 49 into which the upper end of a vertical fall tube fiil'proje cts; Within-the vessel 41 is a'cylindrical "chambervtii having a cooling coil 52 around its ine ans of a pipe 53 and the ends of the cooling "pressure of the refrigerant at its condensing tem- "coil 52 are eonnected to the conduits 21 and 29, "respectively tocause cooling medium to now j therethrough; The top of the chamber 5| is provided with ame asuring orifice 5|a, see Fig. 6,

for deliveringabsorption;solution to the interior of the vessel 4'! at a predetermined fixed "rate The lower anionse which over: the-cooling coil 52;; 'rhe' fall tttbeifill hasiai-relatively small cross 'seotional area so that liquid accumulating in: cup 49 will altern'atelybridge and open the tube as fit flows into the latter and trap. gas between th'e'adja enzhaving the open end; of one-leg 6-1 :at the level a; inthenpper chamber 55'; the reversed bend Slata higher level b in: the upperchamber and the opposite leg -fi3 extending: through the eptum plate toa levei c": the'lower -chamber 56.: Up per chamber-55 is connected to the low pressure side; of the system by a-cond uit 64 'and'in-the illustrated embodiment theconduit is 'connect'ed to the side of theabsorber B. The conduit 64' comprisesa pipe havinga lower closed end 65', see Fig. 2,. andasmaller tube fifi p'rovi'din'g a'gas trap between the pipe. and chamber 55' of the vessel 45 The tube fili -has a depending portion G'linthe-lbwlennd 6 5 of the pipe" and a horizon tal lportion.projecting. through the side wallof the upper chamber- 550f the 'vessel 4B Connected tuthe endor the tube 66 inith'e chamber 55f-.istza'rrlinverted;cuprBB having its-open end po siti'oned; slightly above. the: level a. atrthelowe'r end of therleg 6!. of thezsiphon tube-:60: oThe-cup 68 constitutes; 'apmeasuring device: for V trapping agjpredetermined 1 quantity of gas and together with the depending-leg (1149f the tubexfifilprovides azgas trapin the conduit 64.

Thebottom of the.;lower chamber. 5.6 isconnected'by a conduit l59"-toi thescon'duit. 33-v for deliveringysolution from-theabsorber 8;to the generator-5 Auconduit 10 hasone end, connected to the side of, the lower chamber 56 at the level d and its opposite: end connected to a: gas storage vessel. H; A'suitable means is provided, for emptying the storage vessel .1 I from time to time comprisingiaconduit 12,- valve: 13 and pump". One form of the: inventionhaving no'wybeen .de scribed; inzdetail, themode of operation is ex; plained as follows. 7

V Whenheatingmedium is supplied-to the chamber 14 of the generator 5 its vheat is transmitted through the tubes In toexpelrefrigerant: vapor,- water from absorption solution, lithium bromide solution, and raise the solution in the tubes by vapor lift action. The refrigerant vapor is sepa rated from the absorptions-solution. inthe. sepa-- rating chamber I2 and .fioWs through the con-' duit likinto the condenser 6 where it is liquefied by transferring its heat of vaporization to the cooling-medium flowing through the tubesof the condenser. Liquefied-refrigerant then flows from the.- -condenser. 6 throughv the, conduit I 9 and ori-.- lice Z-Uto the:evaporator 1.

Simultaneously, absorption solution, from p which therefrigerant vaporwhas been expelled fiowsqby gravity through. therconduit -30, heat'xexchanger Strand conduit 31. to the liquid distributing: device-s32 where. it is distributed for flowover the bank-of cooling coils The relatively cool absorption.solutionv absorbsrefrigerant vapor; which reduces theivaporipressure the absorber. hamtevaporator '1. "Theliquidfrefrigerant in: the-tubesfli :of the evaporator 12 then evaporates at the iowerpressureandi temperature to produce. airefrigerating eiiect. Diluted absorption-som tion flows by gravity" from absorber" 8 through the conduit33'; liquid heat exchanger' 9, condui t 34; reservoir vessel 35 and conduit "3'6 'back to the inlet chamber H or the' generator ito completethe'cycle of operation;

Any-liquid refrigerantoverflowi'ng from the lowermost tub'e 2 I of thezevaporator 1 enters the concentration control vessel ill where it" 'is stored in a pressurebalaneing' liquid column: therein-i increase the concentration of the absorption solu-- tion'delivered to; the-absorber B -and thereby-re"- duc'e the pressure; and temperature-of the evapo' ratori'l Any-non-condensablegases occurring in thes stem are deli'r'rered to the absorber 8; Gases in the: generator 5 flow with 'refrigerant' vapor torthe condenser B and'gases-i-n the condenser 6 flow throughthe orifice-'20- to the evaporator: I; Gases-in the evaporator T are swept withthe' refrigerant vapor into the absorber"'8 where. they accumulate at the center and bottom of' the absorber.

Concentrated absorption solution news from conduit 31 into the chamber 5! of purge device 45-through pipe 53 and is delivered'through a measuring Orifice-in the chamber at a predetermined ifixedrate fOl'IfiOW overthe-cooling coil-"52. Thus, the vessel l'l ofthe' purging device '45constitutes an auxiliaryabsorber which absorbs re' f'rigerant vapor therein and creates relative vacuum with respect to themain absorber 8 t'cn'ii 'a-W injnon-condensable gases through the suction tube"48.. The? absorption" solution accumulates in'the sump 48 where it overflows intermittently intorthe fall tubez50 to form successive slugsxof liquid-therein with bubbles of." non-condensable gas" trapped therebetweem The: column of'liquid andgas' in the falltuber libalances the difference in pressure between the vessels 46' and 4"!"andthe addition of liquidat the top of the column in' fall tube causes. acorresponding-amountof liquid tobe delivered from the'fall tubetifl into thenupper chamber 5550f the receiving vesself' lfi;

At the beginning of a: period ofoperation: the gas receiving vessel 46 willbe filledwith: absorption solution standing at the level Yand as the:

} pressure in the absorber decreaseszcolumns ofsolutionwill rise to the level X in conduits 3.3 andi'ii'ill to balance the difference in pressure between-the. generator and absorber; As solution-is delivered fromabsorber 8 into conduit '33 it willfallI to level X and displace a correspondingamount. ofsolution which flows into. reservoir vessel 35. Also solution delivered from the auxiliary absorbervessel 4"! through fall tube 50will displace aucorresponcling amountoi solution fromvessel 46 which flowsthrough conduit 69 to conduit-'33 and into reservoir vessel. 35 but as the solution in fall tube 50 has gas trapped. therein it will be less dense ,andstand at a level higher than the level X in conduit 33 to balance *the' difference. in., pressure. Solution deliveredto the vessel 46* from the fall tube 50lwill'fiow through the stand-'- pi-pe Bl-and: siphon tube 60 to lower chamber 56"then through conduits 69 and-33 towardthe generator 5 and the non-condensable gases will accumulate in the'topvof chamber 55.. This operation will continue .for. a period of time un'tili the accumulated gasesfill the-chamber 55 tothe level a atrwhich time: gas will displace-liqui'd' -m. the cupffifl and will also-break thesiphon in tube 6.0. The absorption liquid then: will accumulate i-nxthe upper chamberfi and rise from 'thelevel 7 a: tothe, level b during which time the gas in chamber 55 will flow through standpipe 51 into chamber 56 and depress the liquid level therein. As the liquid level rises in the chamber 55 the gas trapped in the cup 68 is forced through tube 66 into the lower end of the pipe in conduit 64 and bubbles up through the liquid column therein and into the absorber 8 at the side thereof. When the solution rises to the level 17 in chamber 55 the siphon tube 60 operatesto drain the liquid from the upper chamber into the lower chamber 55. As the liquid level falls from the level I; to the level a in the upper chamber 55v the bottom of the inverted cup 68 is again uncovered and gas enters the cup. Thus, the purge device 45 operates to continuously withdraw noncondensable gases from the low pressure side of the system and the apparatus in the gas receiving vessel 45 operates after a period of time to return gases to the low pressure side of the system at a predetermined rate.

At the end of a period of operation of the system, gases in the vessel 45 will flow back through the fall tube 55, vessel 47 and suction tube 48 into the absorber to provide a quantity of gas to be trapped in solution at the beginning of the next period of operation and the withdrawal from and'return of gas to the absorber 8 is repeated during each cycle of operation. As the liquid in chamber 55 rises from the level a to the level b the gas. therein flows through standpipe and depresses the liquid level in chamber 55 and-when a sufficient amount of gas has accumulated in vessel 46 to depress the liquid to level d, surplus gas will flow into conduit 10, bubble through the liquid therein and enter storage vessel Tl. tion system for a period of time an amount of gas corresponding to the volume of the upper chamber 55 above the level 1) plus a volume in the lower chamber 56 down to level 03 will be available for delivery to the refrigeration system. In this manner accumulation of excessive amounts of gas in the absorber 8 is prevented while the presence of a minimum amount of gas in the absorber is assured to prevent superheating of solution in the generator with its attendant noise and irregular circulation.

Figs. 3 and 4 of the drawings illustrate an apparatus of modified construction for preventing the accumulation of non-condensable gas in the system while at all times maintaining a minimum quantity of gas in the system to prevent superheating of solution in the generator.

ticral with that shownin. Fig. 1 so that the descripion will be limited to the apparatus for con- The refrigeration system illustrated in Fig. 3 is iden- After operation of the refrigera- I trolling the concentration of non-condensable gases in the system. This apparatus comprises agas receiving vessel 15 into which the lower end 16 of the fall tubeiil of the purge device projects. The bottom of the vessel 15,is connected to. solution conduit 33 by a conduit 11. A cup 18in the vessel 15 surrounds the depending end 16 of the fall tube and an auxiliary fall tube '19 extends from a level a at the interior of the cup through the bottom of the vessel and is connected to the side of an upright conduit 80 extending between the conduit 33 and the side of the absorber 8. In the modified construction the lower end of gas overflow pipe 10 projects downwardly into the vessel 15 to a level d below the cup 18. The cup-18 and auxiliary fall tube 19 constitute a secondary purge pump for withdraw- 8 ing, gasjfrom the vessel at a rate which varies with the height of the liquid in the vessel between the level a at the upper end of the auxiliary fall tube 19 and the level (1 at the lower end of the gas overflow pipe 10.

The refrigeration system operates generally in the same way as explained with respect to the apparatus illustrated in Figs. 1 and 2. At the beginning of a period of operation the vessel '15 will be filled with solution to some level slightly above the'end of fall tube 16 with gas trapped in the top'of the vesselabove the liquid level. Any non-condensable gases delivered by the purge device 45 will accumulate at the top ofthe vessel; and displace liquid which flows, therefrom through conduit 11 untilthe liquid falls to the level a. At the beginning of a period of operation the concentration of gases in the absorber 8 will be high so that a relatively large amount of gas will be trapped in solution to insure boilingin the generator 5 without superheat. Also due to the high concentration of gas in the absorber 8 the purge device 45 will withdraw the gas at a relatively high rate but the rate of pumping will decrease proportionately with the concentration of gas- When the liquid in vessel 15 is depressed to some level below the top of the auxiliary fall tube 19 the flow of liquid fromthe primary purge pump 45 through the auxiliary fall tube 19 will start pumping gas from the vessel 15 and deliver it through the upright conduit back to the absorber 8. Pumping is caused by liquid in cup 18 rising around the sides of the auxiliary fall tube 79 until the height of the meniscus is greater than the force of adhesion at which time the liquid bridges and seals the open end of the tube and runs into the latter. When the liquid runs into the tube, it adds weight to the column causing flow in the tube until the liquid in the cup falls to some level below a, due to the cohesion or surface tension of the liquid; at which the liquid film across the top or" the tube breaks. The liquid which last entered the tube will fall to some level between a and the liquid level in vessel 15 depending upon the density of the colurnh and, due to the break in the liquid seal, gas will enter-the end of the tube from the fluid level therein to the level a. When the liquid again rises in cup [8 to a height to bridge the end of the tube it traps the gas between it and the slug of liquid below, the tube being of sufficiently small cross-sectional area so as to prevent gas from ireely bubbling through the liquid. The rate of pumping of gas by fall tube 19 is a function of the difference in height of the liquid columns in the fall tube 79 and vessel 15. This is because the column of fluid in fall tube 19 between level a, and the horizontal portion'of conduit 33 can contain increasing amounts of gas and balance the liquid column in vessel 15 as the liquid levelin'the latter falls. With a greater difference in the height of the liquid columns, a greater amount of gas may be trapped in the solution in fall tube 19 to produce a column of less density in balance with the column of liquid in vessel 15 and conduit 71 above the bottom of the fall tube. Therefore, as the amount of gas in the vessel 15 increases the liquid level in vessel 15 is depressed and the rate of pumping by the auxiliary purge pump "increases until a level is reached at which both purge pumps deliver gas at the same rate. Atsuch time a condition of equilibrium is reached when theconcentration of gasin the absorber is at least suflicient to prevent superheat. Any additional gas will in crease the concentration of gas in the absorber 8 which, in turn, will increase the rate of pumping-by the primary purge device 45 so that more gas will accumulatein the vessel 1-5. This accumulation will continue until the liquid in vessel is depressed to'level d after which gas will be discharged through the conduit 16 to the storage vessel H as fast asit accumulates in the receiving" vessel. Thus, the apparatus operates after a predetermined period of tim to deliver non-condensablegas to the absorber 8 at a predetermined slow rateto insure the presence of a minimum amount of gas in the absorber at all times.

Fig. 5 discloses a secondary purge pump of modified construction which is adapted for use where the quantity of solution delivered by the primary purge device 45 is variable. The construction illustrated in Fig. .5 comprises a gas receiving vessel 85 having a.relatively shallow cup 86 therein, located directly below the end 16 of the fall tube 50. An. auxiliary fall tube '81 has its lower endconnected to the riser conduit 80 as in Fig. 4 but its other end extends-upwardly through the'bottom of the-vessel '85 and cup 86 and terminates above the top of the cup. An orifice 88 is provided in the side .of the auxiliary fall tube 81 which is located at level a between the .top and bottom of the cup 86 and of a size topass liquid at a predetermined rate. A conduit 89 has one end connected to the side of the vessel 85 at level at and its oppositeend connected to the side of an upright conduits!) extending between the solution, conduit 33 and gas storage vessel 1 I.

With the arrangement illustrated in lfig. 5 solution flowing from the primary purge device 45 enters the cup 86 and flows through orifice 88 into the auxiliary fall tube 8.1 at a fixed rate. Flow of solution through the auxiliary fall tube 81 will trap gas entering through its open top and carry it to the conduit 80 where it bubbles through solution and is delivered back to the absorber 8. If the amount of solution delivered from the primary purge device 45 increases it will merely overfiowfrom the cup 86 into vessel 85 without materially-changing the rate of flow through the orifice 88 and fall tube-.81. Gas ac cumulating in vessel 85 displaces solution which flows therefrom through conduits 89' and .99 to conduit 33 and when solution is depressed to level dv gas will escape through saidconduits, rise through the column of solution in conduit 90 and enter storage vessel 1 I.

It-willnow be observed that the. present invention provides apparatus in a two-pressure absorption refrigeration system for controlling the concentration of non-condensable gases in the system. It 'will still further be observed that the present invention provides an apparatus for preventing the-accumulation of excessive amounts of gas in the system while at all times insuring the presence of a minimum amount of gas therein. lt'will still further be observed that the present invention provides an apparatus operable after a predetermined quantity of gas has been withdrawn from the system to deliver measured quantities of the gas back to the low pressure side of :the system at a predetermined slow rate forentrapmentinto solution and deliver excess gasfetoastorage vessel. I

' While three embodiments ofthe invention are herein .illustratedanddescribed, it will be understood that further modifications may be made in the construction and arrangement of elements without departing from the spirit or scope of the invention. Therefore, without limitation in this respect, the invention is defined by the following claims. 7

1. In a vacuum type absorption refrigeration system having a high pressure side and alow pressure side, apparatus for controlling the concentration of non-condensable gas in the .system comprising a vessel for receiving non-conderisable gas, a p-urgedevice for withdrawing non-condensable gas from thelow pressure side and delivering, it to the vessel to prevent the-accumulation'or excessive amounts of gas in the system, and ,conduit means connecting the receiving vessel and low pressure sidezoi the system and constructed to deliver'gas from the receiving vessel backato the low pressure side of the system at a slow-rate to insure the presence of aminimum amquntpf gas in the system. 3

2. In a vacuum type absorption refri eration system having .a generator and condenser operei able at one pressure, and an evaporatorand-abe sorber operable at a lower pressure withzmcans' interconnecting the elements to provide paths of how for refrigerant and absorbent and main-- tain the difference. in pressure, apparatus for-conetrclling the concentration of non-condensable gas in the system comprising avessel for receiving non-,clondensable gas, a purge device connecting to withdraw non-,condensable gas'from the ab! sorber and deliver it to the vessel to 'preventxthe accumulationof an excessive amount ofgasin the absorber, and conduit means directlynonnecting the receiving vessel and absorber ;and .cone structed to operateby the flow ,oflfiuidlimthei system to deliver gas from thereceiving vessel to the absorberat a slow rate toinsure thelpresence of a minimum amount of gas in the absorber.

3. In a vacuum :type absorption refrigeration system having a high pressure side and a, low pressure side, apparatus for controlling'the con centration of'non-condensable gas 'inthe system comprising a gas receiving vessel, a purge device utilizingthe flow of liquid therethrough for withdrawing non-condensable gas from the low pressure side and delivering it-to the vessel to prevent theaccumulation of excessive amounts of gas-in the; system, means utilizing the liquid jro'm the purge device for delivering measured quantities of gas from the-vessel back to the low pressure side to insure the presence ofa minimum amount of gas'in the system, said last named means being so constructedandarranged asto deliver gasat a rate proportional to the rate :at which liquid is delivered from the purge device, and means for controllingthe flow of liquid through-the purge device to maintain the flow of gas to the'lowpres j sure sideat a predeterminedfixed rate.

4. In a vacuum type absorption refrigeration system having a plurality of. elements including n bs rb r interconnectedto provide pathsof flow for refrigerant and absorbent and deliver non-condensable gas to the absorber. apparatus for controlling the, concentration of non-condense able gas in the systemcom rising a gas receiving vessel, a purse device connected to continuously withdraw non-condensable gas from the absorber and deliver itto the gaslreceiving vessel means forv delivering gas at Ya predetermined fixed ,rate from the receiving vessel to the absorberto insure thepresence of a minimum amount .of. gasin the absorber, a gas storage. vessel and meansiior 11 l transferring excess gas to the storage vessel after a predetermined amount has accumulated in the receiving vessel.

, 5. In an absorption refrigeration system, apparatus for controlling the concentration of noncondensable gas in the system comprising a purge device utilizing the flow of liquid therethrough.

forwithdrawing non-condensable gas from the system, a vesselconnected to receive liquid and gas'from the purge device, a siphon tube in the vessel for intermittently draining liquid therefrom to alternately raise and lower the liquid level therein; and conduit means connecting the receiving vessel and low pressure side of the system and constructed to deliver predetermined quantities of gas from the vessel back into the system between the fall and rise of the liquid level in the vessel during each cycle of operation of the siphon.

6. In' a vacuum type absorption refrigeration system having a high pressure side and a low pressure side, apparatus for controlling the concentration of non-condensable gas in the system comprising a purge device utilizing the flowof liquid therethrough for Withdrawing non-condensable gas from the system, a vessel connected to" receive liquid and gas from the purge device, a siphon tube in the vessel for intermittently draining liquid therefrom to alternately raise and lower the liquid level therein, and conduit means connecting the receiving vessel and low pressure side of the system including an inverted cup in th vessel for trapping a measured quantity of gas and delivering the gas from the cup back to the system when the liquid level falls below the bottom of the cup and then rises above the cup durme each siphoning operation.

7. In a vacuum type absorption refrigeration system having a high pressure side and a low pressure side, apparatus for controlling the concentration of non-condensable gas in the system comprising a purge device for withdrawing noncondensable gas from the system, a vessel connected to receive liquid and gas from the purge device, a wall in the vessel separating it into upper and lower chambers with a standpipe eX- tending upwardly from the wall into the upper chamber for permitting the flow of gas between the chambers, a siphon tube connecting the upper and lower chambers for intermittently delivering liquid from the upper chamber to the lower chamber, and a conduit connected between the upper chamber and low pressure side of the system including an inverted cup in the chamber for trapping measured quantitiesof gas and delivering it from the cup back to the system when the liquid level rises in the upper chamber.

8. In an absorption refrigeration system, apparatus for controlling the concentration of'noncondensable gas in the system comprising a gas transfer device utilizing the flow of liquid therethrough for withdrawing gas from the system at a rate varying with the concentration of gas therein, a vessel connected to receive liquid and gas from the gas transfer device, said gas displacing liquid in said vessel, a second gas transfer device in said vessel for withdrawing gas therefrom at a rate varying with the height of the liquid level in the vessel, and a conduit connecting the second gas transfer device to the low pressure side of the system for delivering gas from the second gas transfer device back into the system.

9. In'a vacuum type absorption refrigeration system having a high pressure side and a low pressure side, apparatus for controlling the concentration of non-condensable gas in the system comprising a primary purge device utilizing the flow of liquid therethrough for withdrawing gas from the system, a vessel connected to receive liquid and gas from the primary purge device, a drain conduit through which liquid flows from the vessel back into the system, a secondary purge device in the vessel having a cup underlying the outlet from the primary purge device and a conduit projecting through the bottom of the cup and connected to the system whereby the secondary purge device withdraws gas from the vessel and delivers it back into the system at a rate varying with the height of the liquid level in the vessel to maintain a predetermined minimum amount of gas in the system at all times.

10. 111 a vacuum type absorption refrigeration system having a high pressure side and a low pressure side, apparatus for controlling the concentration of non-condensable gas in the system comprising a primary purge device utilizing the flow of liquid therethrough for withdrawing gas from the system, a vessel connected to receive liquid and gas from the primary purge device, a drain conduit through which displaced liquid flows from the bottom of the vessel back into the system, a secondary purge device in the vessel having a cup underlying the outlet from the primary purge device anda conduit projecting through the bottom of the cup and connected to the system, and a storage tank having a conduit extending into the vessel with its lower end at a level beloW the bottom of the cup.

11. In an absorption refrigeration system, ap-

paratus for controlling the concentration of non-' condensable gas in the system comprising a primary gas transfer device utilizing the flow of liquid therethrough for withdrawing gas from the system, a vessel connected to receive liquid and gas from the primary gas transfer device, and a secondary gas transfer device in the vessel having a fall tube with one end connected to the active part of the system and its opposite end extending through the bottom of the vessel and upwardly above the liquid level therein, said tube having an orifice in the side thereof to deliver liquid at a predetermined fixed rate therethrough whereby the flow of liquid through the orifice traps gas entering through the open end of the fall tube and delivers the gas back to the system.

12. In an absorption refrigeration system, apparatus for controlling the concentration of non condensable gas in the system comprising a primary purge device utilizing the flow of liquid therethrough for withdrawing gas from the system, a vessel connected to receive liquid and gas from the primary purge device, a cup in the vessel, a fall tube having its lower end connected to the system and extending upwardly through the bottom of the vessel and cup with its open end above the liquid level therein, said fall tube having an orifice in the side thereof between the top and bottom of the cup whereby the flow of liquid through the orifice traps gas entering the open end of the tube and delivers the gas back 13 low pressure side of the system and delivering it to the vessel, and a conduit directly connecting the vessel to the low pressure side of the system and having means responsive to the accumulation of a predetermined amount of gas in the I 5 vessel for delivering gas from the receiving vessel Number back to the low pressure side of the system to 942,367 insure the presence of a minimum amount of 2,353,859 gas therein. 2,367,708

NORTON E. BERRY. '10 2,426,069

. 4 REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Name Date Dyer Dec. '7, 1909 Thomas July 18, 1944 Anderson Jan. 23, 1945 Thomas Aug, 19, 1947 

